JP3328749B2 - Method and apparatus for liquefying gas containing low boiling impurities - Google Patents
Method and apparatus for liquefying gas containing low boiling impuritiesInfo
- Publication number
- JP3328749B2 JP3328749B2 JP33144892A JP33144892A JP3328749B2 JP 3328749 B2 JP3328749 B2 JP 3328749B2 JP 33144892 A JP33144892 A JP 33144892A JP 33144892 A JP33144892 A JP 33144892A JP 3328749 B2 JP3328749 B2 JP 3328749B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- liquid
- liquid separator
- liquid separation
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000012535 impurity Substances 0.000 title claims description 16
- 238000009835 boiling Methods 0.000 title claims description 14
- 238000000034 method Methods 0.000 title description 9
- 239000007788 liquid Substances 0.000 claims description 51
- 238000000926 separation method Methods 0.000 claims description 21
- 239000007791 liquid phase Substances 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 53
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 238000011084 recovery Methods 0.000 description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229940110728 nitrogen / oxygen Drugs 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、低沸点不純物を含むガ
スの液化方法に関し、詳しくは、石油化学工業等からの
ガス中に含まれる低沸点不純物と、目的とする主成分ガ
スとを分離して、主成分ガスを液化する方法及び装置に
関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for liquefying a gas containing low-boiling impurities, and more particularly to a method for separating low-boiling impurities contained in a gas from petrochemical industry or the like from a desired main component gas. Thus, the present invention relates to a method and an apparatus for liquefying a main component gas.
【０００２】[0002]
【従来の技術】従来から、石油化学工業等のプラントか
ら導出される各種ガスを精製して液化することが行われ
ている。図３は、低沸点不純物を含むガスを液化する従
来の装置の一例を示すものである。まず、圧縮機１で昇
圧された低沸点不純物を含む原料ガスは、アフタークー
ラー２及び予冷器３で予冷され、更に冷凍機４で冷却さ
れている液化熱交換器５で冷却された後、第１気液分離
器６に導入されて第１次気液分離が行われる。第１気液
分離器６で分離した低沸点成分を多く含む気相は、管６
ａから予冷器３で寒冷を回収された後に排出され、第１
気液分離器６の液相は、調節弁７で減圧された後、第２
気液分離器８に導入されて第２次気液分離が行われる。
第２気液分離器８内の液相は、管８ａを経て製品液化ガ
スとして貯槽に送られ、第２気液分離器８内の気相は、
管８ｂから導出されて予冷器３で寒冷を回収された後に
回収される。2. Description of the Related Art Conventionally, various gases derived from plants such as petrochemical industry have been purified and liquefied. FIG. 3 shows an example of a conventional apparatus for liquefying a gas containing low boiling point impurities. First, the raw material gas containing low-boiling impurities that has been pressurized by the compressor 1 is precooled by the aftercooler 2 and the precooler 3, and further cooled by the liquefaction heat exchanger 5 cooled by the refrigerator 4. It is introduced into the first gas-liquid separator 6 to perform the first gas-liquid separation. The gas phase containing a large amount of low-boiling components separated by the first gas-liquid separator 6 is supplied to a pipe 6
a) is discharged after the cold is recovered from the
After the liquid phase of the gas-liquid separator 6 is depressurized by the control valve 7,
The gas is introduced into the gas-liquid separator 8 to perform a second gas-liquid separation.
The liquid phase in the second gas-liquid separator 8 is sent to the storage tank as a product liquefied gas via a pipe 8a, and the gas phase in the second gas-liquid separator 8 is
It is taken out from the pipe 8b and collected after the cold is collected by the precooler 3.
【０００３】[0003]
【発明が解決しようとする課題】しかしながら、上記従
来の方法では、調節弁７で減圧された後の主成分ガスの
固化を避けるために、第１次気液分離での冷却温度が制
限されてしまう。したがって、第１気液分離器６に導入
する原料ガスの温度を十分に下げることができず、この
状態で分離した気相は、回収可能な主成分ガスを含んだ
まま排出することになり、回収率の向上を妨げる要因と
なっていた。However, in the above-mentioned conventional method, the cooling temperature in the first gas-liquid separation is limited in order to avoid the solidification of the main component gas after the pressure is reduced by the control valve 7. I will. Therefore, the temperature of the raw material gas introduced into the first gas-liquid separator 6 cannot be sufficiently lowered, and the gas phase separated in this state is discharged while containing the recoverable main component gas, This was a factor that hindered the improvement of the recovery rate.
【０００４】そこで本発明は、第１次気液分離での冷却
温度の制限をなくすことにより、回収率の向上を図れる
低沸点不純物を含むガスの液化方法及び装置を提供する
ことを目的としている。Accordingly, an object of the present invention is to provide a method and an apparatus for liquefying a gas containing low-boiling-point impurities, which can improve the recovery rate by eliminating the limitation of the cooling temperature in the first gas-liquid separation. .
【０００５】[0005]
【課題を解決するための手段】上記した目的を達成する
ため、本発明の低沸点不純物を含むガスの液化方法は、
低沸点不純物を含む原料ガスを昇圧して冷却した後、第
１次気液分離を行い、次いで、分離した液相を昇温した
後、減圧して第２次気液分離を行い、分離した液相を採
取することを特徴としている。In order to achieve the above-mentioned object, a method for liquefying a gas containing low-boiling impurities according to the present invention comprises:
After the raw material gas containing the low-boiling impurities is pressurized and cooled, first gas-liquid separation is performed. Then, after the separated liquid phase is heated, the pressure is reduced and the second gas-liquid separation is performed. It is characterized by collecting the liquid phase.
【０００６】また、本発明の低沸点不純物を含むガスの
液化装置は、低沸点不純物を含む原料ガスを圧縮する圧
縮機と、昇圧後の原料ガスを冷却する冷却器と、冷却後
の原料ガスの気液分離を行う第１気液分離器と、該第１
気液分離器で分離した液相を加温する加温器と、加温器
で加温された原料ガスを減圧する調節弁と、減圧後の原
料ガスの気液分離を行う第２気液分離器とを備えたこと
を特徴としている。Further, the liquefaction apparatus for a gas containing low-boiling impurities according to the present invention comprises a compressor for compressing a source gas containing low-boiling impurities, a cooler for cooling the source gas after pressurization, and a source gas after cooling. A first gas-liquid separator for performing gas-liquid separation of
A heater for heating the liquid phase separated by the gas-liquid separator, a control valve for reducing the pressure of the source gas heated by the heater, and a second gas-liquid for performing gas-liquid separation of the source gas after the pressure reduction And a separator.
【０００７】[0007]
【作 用】上記構成によれば、第２次気液分離を行うた
めの調節弁での減圧の前に原料ガス（第１気液分離器で
分離した液相）を昇温するので、第１気液分離における
冷却温度を低く設定することができ、第１気液分離器か
ら排出される気相中に含まれる主成分ガス量を低減して
得られる液相を増加させることができる。したがって、
排出される主成分ガス量の低減により製品の回収率の向
上が図れる。According to the above configuration, the temperature of the raw material gas (the liquid phase separated by the first gas-liquid separator) is increased before the pressure is reduced by the control valve for performing the second gas-liquid separation. The cooling temperature in one gas-liquid separation can be set low, and the liquid phase obtained by reducing the amount of the main component gas contained in the gas phase discharged from the first gas-liquid separator can be increased. Therefore,
By reducing the amount of the main component gas discharged, the recovery rate of the product can be improved.
【０００８】[0008]
【実施例】以下、本発明を、図面に示す一実施例に基づ
いてさらに詳細に説明する。図１は、本発明の液化装置
の一例を示す系統図であって、原料ガスを昇圧する圧縮
機１１と、昇圧した原料ガスを冷却するためのアフター
クーラー１２，第１熱交換器１３，第２熱交換器１４及
び液化熱交換器１５と、第１気液分離器１６と、調節弁
１７と、第２気液分離器１８とから構成されている。DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below in more detail with reference to an embodiment shown in the drawings. FIG. 1 is a system diagram showing an example of the liquefaction apparatus of the present invention, which includes a compressor 11 for increasing the pressure of a raw material gas, an aftercooler 12 for cooling the raised raw material gas, a first heat exchanger 13, It is composed of two heat exchangers 14, a liquefaction heat exchanger 15, a first gas-liquid separator 16, a control valve 17, and a second gas-liquid separator 18.
【０００９】管２１から供給される原料ガス、例えば、
低沸点不純物として窒素１９％，酸素１％を含む炭酸ガ
スは、回収回路である管２２からの回収ガス（炭酸ガス
約８８％，窒素約１１％，酸素約１％）と合流し、炭酸
ガス約８１％，窒素約１８％，酸素約１％となった後、
圧縮機１１で所定の圧力、例えば約２０ｋｇ／ｃｍ2Ｇ
まで昇圧される。A source gas supplied from the pipe 21, for example,
Carbon dioxide containing 19% of nitrogen and 1% of oxygen as low-boiling-point impurities is combined with a recovery gas (about 88% of carbon dioxide, about 11% of nitrogen, and about 1% of oxygen) from a pipe 22 as a recovery circuit to form carbon dioxide After about 81%, about 18% nitrogen and about 1% oxygen,
A predetermined pressure, for example, about 20 kg / cm 2 G in the compressor 11
Up to
【００１０】昇圧された原料ガスは、アフタークーラー
１２，第１熱交換器１３，第２熱交換器１４及び液化熱
交換器１５で順次冷却されて−５０℃になり、一部が液
化した状態で第１気液分離器１６に導入される。この第
１気液分離器１６における第１次気液分離で分離した気
相は、組成が炭酸ガス約４０％，窒素約５７％，酸素約
３％であり、管２３に導出されて第２熱交換器１４及び
第１熱交換器１３で寒冷を回収された後、パージガスと
して排出される。The pressurized raw material gas is sequentially cooled by an aftercooler 12, a first heat exchanger 13, a second heat exchanger 14, and a liquefaction heat exchanger 15 to -50.degree. C., and is partially liquefied. At the first gas-liquid separator 16. The gas phase separated by the first gas-liquid separation in the first gas-liquid separator 16 has a composition of about 40% of carbon dioxide, about 57% of nitrogen and about 3% of oxygen. After the cold is recovered by the heat exchanger 14 and the first heat exchanger 13, the gas is discharged as a purge gas.
【００１１】第１気液分離器１６内の液相は、管２４に
より第２熱交換器１４に導入されて再熱された後、調節
弁１７で約７ｋｇ／ｃｍ2 Ｇまで減圧し、温度が−５０
℃まで低下して一部が液化した状態で第２気液分離器１
８に導入される。この第２気液分離器１８における第２
次気液分離で分離した液相は、その組成が炭酸ガス約９
９．８％，窒素約０．１６％，酸素約０．０４％であ
り、管２５から導出されて貯蔵される。一方の気相は、
前記回収ガス（炭酸ガス約８８％，窒素約１１％，酸素
約１％）となり、管２６に導出されて第２熱交換器１４
及び第１熱交換器１３で寒冷を回収された後、前記管２
２を経て原料ガスに合流する。The liquid phase in the first gas-liquid separator 16 is introduced into the second heat exchanger 14 through a pipe 24 and reheated. Then, the pressure is reduced to about 7 kg / cm 2 G by the control valve 17 and the temperature is reduced. Is -50
The second gas-liquid separator 1 is cooled down to
8 is introduced. The second gas-liquid separator 18
The liquid phase separated by the secondary gas-liquid separation has a composition of about 9% carbon dioxide.
It is 9.8%, about 0.16% nitrogen and about 0.04% oxygen, and is discharged from the tube 25 and stored. One gas phase is
The recovered gas (carbon dioxide gas: about 88%, nitrogen: about 11%, oxygen: about 1%) is led out to the pipe 26 and is discharged to the second heat exchanger 14
And after the cold is recovered in the first heat exchanger 13, the pipe 2
And joins the raw material gas through 2.
【００１２】なお、第２熱交換器１４では、該第２熱交
換器１４を導出して調節弁１７で減圧した後の第２気液
分離器１８の入口温度を、主成分ガスの固化点に近い温
度に調節するため、必要に応じて温流体である原料ガス
ラインにバイパス弁２７を有するバイパス管２８を設
け、第２熱交換器１４における熱交換量を調整できるよ
うにすることが好ましい。In the second heat exchanger 14, the inlet temperature of the second gas-liquid separator 18 after the second heat exchanger 14 is led out and depressurized by the control valve 17 is set to the solidification point of the main component gas. In order to adjust the temperature to a temperature close to the above, it is preferable to provide a bypass pipe 28 having a bypass valve 27 in the raw material gas line, which is a hot fluid, if necessary, so that the heat exchange amount in the second heat exchanger 14 can be adjusted. .
【００１３】このように、第１気液分離器１６から導出
した液相を、そのまま減圧せずに適当な温度にまで加温
した後に減圧するようにしたことにより、第１次気液分
離の際の冷却温度を、低沸点不純物を分離するのに最適
な温度にすることが可能になり、パージガス中に排出さ
れる主成分ガスの量を低減して製品液化ガスとして採取
する量を増大することができる。As described above, the liquid phase led out of the first gas-liquid separator 16 is heated to an appropriate temperature without being depressurized as it is, and then depressurized. In this case, the cooling temperature can be adjusted to an optimum temperature for separating low-boiling impurities, thereby reducing the amount of the main component gas discharged in the purge gas and increasing the amount collected as the product liquefied gas. be able to.
【００１４】図２は、本発明法と従来法とにおける原料
ガスの圧力と回収率及び所要動力原単位を示すもので、
図から明らかなように、本発明法によれば、回収率の大
幅な向上と所要動力原単位の低減を図れることが判る。FIG. 2 shows the source gas pressure, the recovery rate, and the required power consumption in the method of the present invention and the conventional method.
As is apparent from the figure, according to the method of the present invention, it is possible to significantly improve the recovery rate and reduce the required power consumption.
【００１５】なお、装置構成は、上記実施例に限定され
るものではなく、例えば気液分離器の設置数を、３基以
上にすることも可能であり、この場合も減圧前に加温す
る工程を行うことにより、前段の気液分離工程の温度を
任意に設定することが可能になり、回収率の向上が図れ
る。また、上記実施例では、第１気液分離の際には、そ
のままの圧力で気液分離を行うようにしたが、第１気液
分離器の前段に調節弁を設け、減圧してから第１次気液
分離を行うように構成することもできる。さらに、原料
ガスの組成は、上記窒素・酸素−炭酸ガスに限らず、例
えば、窒素，酸素，水素等の低沸点成分を不純物として
含んだエタン，プロパン，二酸化硫黄等の液化にも適用
することができる。The configuration of the apparatus is not limited to the above embodiment. For example, the number of gas-liquid separators can be set to three or more. In this case, heating is performed before the pressure is reduced. By performing the step, it is possible to arbitrarily set the temperature of the preceding gas-liquid separation step, and it is possible to improve the recovery rate. Further, in the above embodiment, the gas-liquid separation is performed at the same pressure at the time of the first gas-liquid separation. However, a control valve is provided before the first gas-liquid separator, and the pressure is reduced after the pressure is reduced. It may be configured to perform primary gas-liquid separation. Further, the composition of the raw material gas is not limited to the above-described nitrogen / oxygen / carbon dioxide gas, but may be applied to, for example, liquefaction of ethane, propane, sulfur dioxide and the like containing low boiling components such as nitrogen, oxygen and hydrogen as impurities. Can be.
【００１６】[0016]
【発明の効果】以上説明したように、本発明によれば、
前段の気液分離器から導出した液相を一旦加温してから
減圧するようにしたので、前段の気液分離における温度
制限を無くすことができ、主成分ガスの固化点付近まで
冷却することが可能になり、前段の気液分離器で気相中
に分離する主成分ガスの量を低減させ、製品として回収
する主成分ガスの量を大幅に増大させることができる。
さらに、回収率の向上に伴って所要動力原単位が低下
し、製品コストの大幅な低減が可能になる。As described above, according to the present invention,
Since the liquid phase derived from the gas-liquid separator at the previous stage is once heated and then decompressed, the temperature limitation in the gas-liquid separation at the previous stage can be eliminated, and it can be cooled to around the solidification point of the main component gas. It is possible to reduce the amount of the main component gas separated into the gas phase in the gas-liquid separator at the preceding stage, and to greatly increase the amount of the main component gas recovered as a product.
Furthermore, the required power consumption decreases with the improvement of the recovery rate, and the product cost can be significantly reduced.
【図１】 本発明の一実施例を示す液化装置の系統図で
ある。FIG. 1 is a system diagram of a liquefaction apparatus showing one embodiment of the present invention.
【図２】 本発明法と従来法とにおける原料ガスの圧力
と回収率及び所要動力原単位の関係を示す図である。FIG. 2 is a diagram showing a relationship between a pressure of a raw material gas, a recovery rate, and a required power consumption unit in the method of the present invention and the conventional method.
【図３】 従来の液化装置の一例を示す系統図である。FIG. 3 is a system diagram showing an example of a conventional liquefaction apparatus.
１１…圧縮機、１２…アフタークーラー、１３…第１熱
交換器、１４…第２熱交換器、１５…液化熱交換器、１
６…第１気液分離器、１７…調節弁、１８…第２気液分
離器11: Compressor, 12: Aftercooler, 13: First heat exchanger, 14: Second heat exchanger, 15: Liquefaction heat exchanger, 1
6 first gas-liquid separator, 17 control valve, 18 second gas-liquid separator
Claims (2)
冷却した後、第１次気液分離を行い、次いで、分離した
液相を昇温した後、減圧して第２次気液分離を行い、分
離した液相を採取することを特徴とする低沸点不純物を
含むガスの液化方法。1. A first gas-liquid separation is performed after a raw material gas containing a low boiling point impurity is pressurized and cooled, and then the separated liquid phase is heated and then decompressed to a second gas-liquid separation. And collecting a separated liquid phase.
圧縮機と、昇圧後の原料ガスを冷却する冷却器と、冷却
後の原料ガスの気液分離を行う第１気液分離器と、該第
１気液分離器で分離した液相を加温する加温器と、加温
器で加温された原料ガスを減圧する調節弁と、減圧後の
原料ガスの気液分離を行う第２気液分離器とを備えたこ
とを特徴とする低沸点不純物を含むガスの液化装置。2. A compressor for compressing a source gas containing low-boiling impurities, a cooler for cooling the source gas after pressurization, a first gas-liquid separator for gas-liquid separation of the cooled source gas, A heater for heating the liquid phase separated by the first gas-liquid separator, a control valve for reducing the pressure of the source gas heated by the heater, and a second valve for performing gas-liquid separation of the source gas after the pressure reduction. A gas liquefaction apparatus comprising a low-boiling-point impurity, comprising a two-gas-liquid separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33144892A JP3328749B2 (en) | 1992-12-11 | 1992-12-11 | Method and apparatus for liquefying gas containing low boiling impurities |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33144892A JP3328749B2 (en) | 1992-12-11 | 1992-12-11 | Method and apparatus for liquefying gas containing low boiling impurities |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06194036A JPH06194036A (en) | 1994-07-15 |
| JP3328749B2 true JP3328749B2 (en) | 2002-09-30 |
Family
ID=18243769
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP33144892A Expired - Fee Related JP3328749B2 (en) | 1992-12-11 | 1992-12-11 | Method and apparatus for liquefying gas containing low boiling impurities |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3328749B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TR199801906T2 (en) * | 1996-03-26 | 1999-01-18 | Phillips Petroleum Company | Removal of aromatic substances and/or heavy substances by condensation and stripping from a methane-based feed. |
| CZ297345B6 (en) * | 2001-10-16 | 2006-11-15 | Ateko, A. S. | Apparatus for low-temperature separation of gas |
| CN106052300B (en) * | 2016-05-30 | 2019-02-05 | 中国科学院理化技术研究所 | Gas purification system |
| FR3088416B1 (en) * | 2018-11-08 | 2020-12-11 | Air Liquide | METHOD AND APPARATUS FOR LIQUEFACTION OF A GAS CURRENT CONTAINING CARBON DIOXIDE |
-
1992
- 1992-12-11 JP JP33144892A patent/JP3328749B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH06194036A (en) | 1994-07-15 |
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